JP2002522213A - Method and assembly for separating solids from the gas phase - Google Patents

Abstract

The invention relates to a method for separating materials of two different phases from one another and an assembly for implementing the method. According to one embodiment of the invention, the second phase having the material in suspended or dispersed form is separated from the first phase by centrifugal force. At least one separator comprises a multiport cyclone into which the material flow is passed via an infeed nozzle having an annular cross section.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

FIELD OF THE INVENTION

The present invention relates to a method for separating two phases from each other and to an assembly suitable for carrying out this method. The invention particularly relates to a method for separating solids and / or liquids from a gas stream or for separating solids from a liquid stream according to the preamble of claim 1. In the method of the present invention, a gas stream containing catalysts and other solids is passed through a separation means, where the other phases are separated from the gas stream by the action of centrifugal force. Similarly, when separating solids from the liquid phase, the liquid stream is passed through a separator and the solids are separated from the liquid phase by the action of centrifugal force. The invention further relates to an apparatus for separating solids and / or liquids from a gas / liquid stream of a fluidized bed according to the preamble of claim 15.

[0002]

[Prior art]

The most commercially valuable embodiment used to separate the two phases is a fluidized bed reactor. Fluid bed reactors are commonly used in hydrocarbon conversion processes and energy generators. In these devices, the catalyst or solid material for better heat transfer or fluidization of the material is kept fluidized by a gaseous hydrocarbon or flue gas stream. Thereafter, the solids are separated from the gas stream using a cyclone. The most common fluidized bed reactor is a bubbling bed reactor, where the linear flow rate of the fluidizing medium is 5 to 10 times the minimum fluidization rate capable of maintaining a major portion of the solids in the fluidized bed of the reactor. And substantially no solids are lost from the reactor along with the hydrocarbon and flue gas streams. The term minimum bubbling velocity refers to the linear gas velocity at which a portion of the gas stream begins to pass through the fluidized bed in a bubbling state. This minimum bubbling rate depends on the flowing gas and the properties of the solid.

When the gas flow rate becomes faster than the minimum bubbling rate, the upper part of the fluidized bed deforms irregularly and enters a gradient zone in which the solids content decreases upstream. When the flow rate is further increased, fluidization occurs, and almost all solid particles are entrained in the gas flow, and the fluidized state is maintained. Thereafter, the solids entrained in the gas stream must be separated from the gas stream in a cyclone and the separated solids must be returned to the bottom of the reaction space so that the mass balance does not change. The method and assembly of the present invention can be used in hydrocarbon treatment processes and the like.
Examples of such processes are catalytic cracking, thermal cracking, dehydrogenation, Fischer-Tropsch synthesis, production of maleic anhydride and oxidative dimerization of methane.

[0004] A fluidized bed reactor commonly used in the field of energy generation is a boiler. In this case, a fluidizing material such as sand and / or solid fuel particles are fluidized by the combustion air stream and the flue gas emitted in this process. Liquid or gas phase fuels can also be used. Conventionally, both circulating fluidized beds (C
FB) reactors are commonly used. Again, solids and unburned particles are removed from the flue gas stream by a cyclone. The term entrained fluidization refers to fluidization that occurs in both the turbulent high speed fluidization zone and the pneumatic transfer zone. The hydrocarbon conversion process is carried out using a fixed bed reactor and a fluidized bed reactor (fluidized catalytic reactor). In the present invention, a "fluidized catalyzed process device"
The term "tic process equipment" refers to equipment used in a process in which a finely divided catalyst is suspended in a slowly rising gas stream, where the catalyst facilitates the desired reaction.

[0005] One of the most widely used fluid catalytic reactor systems in the prior art is the FCC unit. This is a fluidized catalytic cracking device consisting mainly of a riser pipe acting as a reactor operated in a high-speed fluidized flow state and a regenerator operated in a high-density bubbling bed state. In a fluidized bed reactor, product gas is separated from suspended solid particulate matter in a cyclone using the action of centrifugal force. Since a cyclone having a general structure has poor separation ability with respect to particles having a size of 15 μm or less, it is necessary to connect a plurality of cyclones in series along a gas flow to improve the overall recovery efficiency. A single cyclone is more efficient if small diameter particles can be separated from the gas stream.

[0006] Cyclones are not only used in fluidized bed reactors, but also for example the separation of droplets from streams, the separation of solids from flue gases in drying processes, the separation of two-phase streams (demister devices), the gas It is also used for separation of solids from wastewater (Chile separator) and crude separation of solids from wastewater (liquid cyclone). The cyclone separator has a coiled or helical configuration, and the particulate suspension flows tangentially into the cylindrical portion of the cyclone and passes through the inside of the cylindrical portion of the cyclone and the conical portion of its extension generally about 7 to 9 times. During rotation, the catalyst particles are separated from the gas,
Transported near the inner wall of the cyclone. There is also known an axial cyclone in which gas flowing in a pipe is forcedly circulated by a blade, and centrifugal force generated thereby pushes a solid against a pipe wall to separate the solid from a gas flow.

[0007] The most common type of cyclone is a single-port helical cyclone called the Zenz cyclone. In this cyclone, dimensions of each part of the cyclone are standardized, and a desired cyclone dimension can be determined based on a graph and a calculation formula. To increase the cyclone recovery efficiency, the rotation speed of the flow in the cyclone chamber is increased, the flow velocity of the inlet nozzle is increased, the solid density is increased, the inlet nozzle is narrowed, and the viscosity of the gas is reduced. From tests of the pre-separation cyclone of the fluidized catalytic cracking facility, the residence time of the gas from the top of the riser to the cyclone outlet was 1.0-2.0 seconds, after which the catalyst was placed in the heated separation vessel for another 5 seconds. It was found to stay for ~ 40 seconds.
During this residence time, important compounds in the gas are lost by the heating reaction. That is, the gasoline product by pyrolysis combustible gas, varies in particular C ₂ type hydrocarbons. Another by-product of the thermal reaction is a diene, such as butadiene, which greatly increases the acid consumption in the alkylation facility. Pentadiene is highly reactive, FC
C significantly reduces the oxidation resistance of gasoline. Problems that make cyclones unusable in conventional FCC facilities are the difficulty in controlling the reaction time and the erosion of the catalyst particles / circulating solids and the reaction structure.

[0008]

[Problems to be solved by the invention]

These problems mainly concern the main part of the device or cyclone for separating the gas from the solid / catalyst. That is, most conventional cyclones have been single-port cyclones. Single-port cyclone means a cyclone structure with only one inlet nozzle for supplying a gas stream to the cyclone. In this case, a plurality of units are generally connected in parallel to obtain a desired flat processing capacity.
Are connected in series. Such a conventional cyclone structure is not only complicated and expensive, but also requires a large installation area. In addition, the cyclone interior space must be lined with ceramic to prevent erosion. It is an object of the present invention to provide a completely new method and assembly for separating solids from a gas stream which overcomes the above disadvantages.

[0009]

[Means to solve the problem]

The above object of the present invention is to provide at least one of the conventional cyclones for fluidized catalytic processes
This is achieved by replacing one with a cyclone having a plurality of inlets (also called a multi-inlet cyclone or a multi-port cyclone) or a plurality of the multi-port cyclones connected in series with one another. Here, the term multiport cyclone refers to a cyclone structure having at least two, preferably four to eight, inlet ports and allowing the gas flow to flow substantially tangentially over the inner wall of the cyclone. The structure of the multi-port cyclone is simpler than conventional cyclones, can be cheaper, can provide higher recovery efficiency even at low speeds, and requires a smaller site area.

[0010]

Embodiment

The multi-inlet cyclone was a 1974 DuPont (EI Du Pont de Nemou
(rs and Company) in U.S. Pat. No. 3,969,096.
The cyclone separator described in this patent has a plurality of vaned gas inlet openings. This cyclone is used to separate suspended particles from the exhaust gas of an internal combustion engine (automobile). However, the Dupont patent does not provide a theoretical explanation for why the multiport cyclone provides excellent recovery efficiency at low pressures. According to their hypothesis, the inlet guide vanes supply a sheet-like stream of gas entering the cyclone separator near the inner wall of the cyclone. Thus, the entrained particles need only travel a short distance before separation. The inventor of this patent further assumes that the sheet-like inlet fluid forms a sharp demarcation between the lower and upper vortices, and the gas flow is less likely to form vortices. As mentioned in the specification of this patent, reducing the formation of vortices reduces the drag that slows the flow and increases the separation efficiency.

[0011] The separation device or cyclone used in the present invention comprises a cyclone separation chamber having at least a substantially vertically aligned central axis, the interior space of which is preferably substantially annular in cross section, with respect to the central axis. And preferably rotationally symmetric. A supply nozzle for the process gas is connected to the separation chamber and has a substantially annular cross section about the central axis of the separation chamber. The separation chamber further includes a central pipe for discharging gas and a downward return lug for collecting solids separated from the gas phase. The separation chamber comprises a set of blades forming a louver, which forces the gas into a circulating stream near the inner wall of the cyclone chamber to separate solids from the gas phase under the action of centrifugal force.

[0012] Preferably, the assembly of the present invention comprises cylindrical shells arranged coaxially with one another, such that the passage between each shell having an annular cross section serves as a flow space and a return lug. The catalyst or solids are separated from the gaseous suspension leaving the reactor via a multiport cyclone located directly above the axial annular shell-to-shell flow path. The term "solid" means a material that forms a suspension in the reaction space. Generally, in a reactor utilizing a catalytic reaction, the solid consists of catalyst particles. When the reactor uses a physical or thermal process, the solid is an inert particulate material that serves to supply heat or material into or out of the reaction space, or is a solid fuel particle. The catalyst is chosen according to the process used.

The multi-port cyclone is preferably connected to the upper part of the reaction space. The material to be processed in the cyclone is sent to the chamber through a plurality of inlet openings. The entrance openings are symmetrically or asymmetrically arranged around the central axis of the cyclone. Preferably, the openings are arranged symmetrically and the riser space has an annular cross-section, whereby the gas flow is uniform over the entire cross-section of the flow path. In this case, the cyclone is provided with gas flow guide vanes, which serve to give the gas flow the helical movement required for centrifugation. Generally, the guide vanes are provided in a circular louver shape around the inner wall of the cyclone chamber so as to form a louver having a plurality of parallel inlet passages for an incoming gas flow. Accordingly, the supply nozzle of the multi-port cyclone is provided with means for deflecting the supply flow radially entering the cyclone. This means serves to direct the gas flow from the periphery of the cyclone to the center of the cyclone, for example by means of at least a part of the vane region which deflects the impinging flow, so as to direct the gas flow from the periphery of the cyclone to the center of the cyclone. Guide vanes or the like provided on the upper part.

A CYMIC circulating bed boiler developed by Kvaeruner Pulping Oy (predecessor of Tampella Power Oy) uses this multiport cyclone to remove associated particles of fluidized bed material from flue gas to remove particulate matter. Returning to boiler.
The cyclone is located in the interior space of the boiler and is cooled with water. A second multiport cyclone can be provided in the interior space of the first or conventional cyclone as long as the gas flow in the cyclone is symmetric and the flow can be symmetrically distributed to the guide vanes of the second cyclone. It is. When the catalyst concentration of the second cyclone is low, this type of arrangement provides favorable flow and structural characteristics, since the second cyclone can be operated at a higher flow rate than the previous upstream cyclone. The desired number of cyclones can be connected in series depending on available factory space and recovery efficiency.

In a preferred embodiment of the invention, a supply nozzle of substantially annular cross section is used to disperse the gas to be treated, and the means for deflecting the radially flowing gas flow are radially outward from the outer periphery of the cyclone. Extending. In a particularly preferred embodiment of the invention, said means, such as feed nozzles with guide vanes, extend downwardly from the upper level of the cyclone along the outer circumference of the shell of the cyclone from the upper level of the cyclone. The guide vane portion is located on the outer surface of the cyclone and faces downward and directs the gas flow entering the cyclone upwardly from the cyclone surrounding the cyclone. In the context of the present invention, the direction of flow is used, for example, to refer to the direction in which the flow is guided, stabilized and / or deflected. The guide vanes may be only partially installed inside the inlet lug, or may be completely or partially installed inside the cyclone.

In the preferred embodiment of the present invention, each downward return lug of the cyclone provided coaxially is similarly coaxially installed. In a further preferred embodiment of the invention having at least two coaxially arranged cyclones, the cyclone is designed such that any inner cyclone guide vane is always located above the front upstream cyclone guide vane. Is preferred. Accordingly, the object of the present invention is achieved by placing at least one second multi-port cyclone inside a first cyclone or other preceding second cyclone. In particular, the method is characterized by the features of claim 1. Furthermore, the assembly according to the invention is characterized by the features of claim 15.

The present invention has many advantages. The structure of the device according to the invention, based on a multi-port cyclone, offers significant advantages over the hydrodynamic and process engineering of conventional and commonly used single-port cyclones. That is, in the conventional single-port cyclone, the solid stream collides with the inner wall of the cyclone as a uniform gas suspension jet having a high flow velocity, and the flow velocity is generally in the range of 20 to 25 m per second in the first cyclone.
The second cyclone is about 35 meters per second and the third cyclone is about 40 meters per second.
Also, the cyclone inlet nozzle width (jet width) is typically, for example, about one-fourth the diameter of the cyclone in a standard Zenz cyclone, and the particulate matter must cover the entire impingement jet width to achieve separation of solids from the gas stream. Must be carried near the inner wall of the cyclone, so that the impinging jet must have a high flow rate. However, the most susceptible location for this type of cyclone is the inner wall region of the cyclone which is subjected to jet impact of suspended catalyst particles.

In contrast, in the structure of the present invention, the problem of erosion is eliminated by improving the fluid dynamics. Erosion is spread over a large area by dividing a conventional single large volume inlet solids stream into multiple smaller volumes to impinge on the inner wall of the multiport cyclone. The multi-port configuration allows for a narrow cyclone inlet port, which results in a shallower catalyst phase and lower flow rates at any inlet port than in conventional single-port cyclones. In a single-port cyclone, reducing the width of the inlet port requires an increase in lug height, which results in a tall cyclone and a longer, ugly feed lug. In the present invention, since the cyclone inlet flow velocity can be reduced, the erosion rate is further reduced. According to the literature, the erosion rate is proportional to the fourth to fifth power of the flow rate.

A 465 mm diameter cyclone having a full area inlet port and straight blades
. The recovery efficiency was 99.99% when tested at room temperature at a cross-sectional weight flow rate of the catalyst such that the measured pressure difference was 200 kg / m ² seconds or more at an inlet flow rate of 6 m. The recovery efficiency calculated from the particle size fraction when a conventional Zenz cyclone having equivalent dimensions was operated at the same flow rate was 99.10%. By comparing the recovery efficiencies of both, if the design objective is to avoid high-velocity flow causing erosion, the new cyclone with multiple narrow inlet ports of the present invention will provide better efficiency It turns out that.

In the preferred structure of the present invention, in which the reactor riser pipe (hereinafter simply referred to as “riser”) is directly connected to the cyclone inlet pipe, the residence time is precisely controlled because the catalyst enters the cyclone simultaneously from each position of the supply pipe. It becomes possible to do. The cyclones of the present invention can be designed to have about half the capacity of a standard cyclone. By installing the cyclones coaxially with each other, the internal capacity of the cyclone pressure vessel can be greatly reduced as compared with the case where the cyclones are installed in a parallel or overlapping manner in the internal space of the pressure vessel. Due to the hydrodynamic advantages of the cyclones of the present invention, shorter structures can be used, and their height and residence time can be, for example, half that of a standard cyclone. As a result, undesirable thermal reactions are reduced. Furthermore, if necessary, the product can be cooled directly in the cyclone discharge pipe.

In a first preferred embodiment of the present invention, a multiport cyclone is used to separate the catalyst from the product gas of a fluid catalytic cracking (FCC) process. This multi-port cyclone can also be used to separate the regenerated catalyst from the coke combustion gas in the heat exchange device of the FCC unit. Other fluid catalytic methods include catalytic reforming, oxidative dimerization of phthalic anhydride, maleic anhydride or methane, Fischer-Tropsch synthesis, chlorination and bromination of methane, ethane, and other hydrocarbons, and olefins or gasoline of methanol The conversion to can be raised.

The separation of solids can be carried out in a plurality (eg 2 to 10, most suitably 2 to 5) connected in series.
) Cyclone. In this case, according to the invention, at least one is a multi-port cyclone and the other cyclones can be arranged coaxially inside one another. For example, a downward return lug of any one cyclone of the downstream cyclone is provided inside the downward return lug of the preceding cyclone. By arranging each cyclone coaxially in the pressure vessel, the capacity can be greatly reduced as compared with the conventional cyclone structure in which cyclones must be arranged in parallel. While the diameter of a conventional cyclone is generally limited to a maximum of 1 m, a multi-port cyclone can be made larger in diameter than a conventional cyclone, and the diameter of a multi-port cyclone can be greater than one meter and less than a few meters. However, in the embodiment of the present invention, the diameter of the reaction vessel does not need to be increased, but can be reduced.

The cyclone feed nozzle can be formed in the interstitial space between two coaxially provided cylindrical or partially conical outer surfaces. This annular space can also be divided into parallel substreams using axially extending baffles. This parallel split flow is obtained by mounting a radial baffle between two coaxially arranged cylindrical surfaces in longitudinal alignment. Approximately the same result is obtained when a group of parallel supply tubes are installed at equal intervals in a circular shape on a supply nozzle having an annular cross section. The guide vanes of the cyclone may be partially or entirely provided inside the riser lug in a circular louver shape on the outer periphery of the cyclone chamber to form a louver having a plurality of parallel inlet lugs into which a gas flow enters.

The cyclone of the present invention may be directly connected to a riser lug (referred to simply as a riser) of a fluidized catalytic reactor, which is a preferred embodiment of the present invention, or a cyclone feed nozzle may be connected to a fluid catalyst as in a conventional arrangement. To the gas space of the process reactor. A preferred embodiment of the invention comprises means for radially deflecting the flow entering the cyclone which is arranged to extend radially outward towards the outer space of the cyclone. By this means the flow can be effectively controlled before entering the cyclone. In a particularly advantageous embodiment of the invention, this means extends downward from the top of the cyclone to further enhance the effect of controlling the flow and to start controlling the flow earlier than in the prior art. As a result, it is possible to effectively and early control the flow leaving the vortex region of the outer cyclone in the preceding stage. Due to this effective flow control structure, the flow is desirably directed to the inner cyclone and is not affected by irregular flow patterns of the outer cyclone. Furthermore, a better than expected excellent pre-separation can be facilitated in the outer vertical part of the inner cyclone between the outer cyclone and the inner cyclone of the assembly due to the strong flow control effect provided by the guide vanes. If the inlet flow to the inner cyclone already has a tangential velocity component, it is advantageous not to extend the guide vanes to the outer end of the inner cyclone inlet lug.

Yet another advantage is obtained by means of vertical deflection or guidance provided on the outer circumference of the cyclone. This deflecting or guiding means consists of a tubular outer surface forming a gas flow passage in the interstitial space between the outer surface and said outer periphery of the inner surface, whereby the multi-port cyclones are coaxially mounted on one another and a series of inner cyclones are provided. Is easier to locate above the outer cyclone guide vanes. It is easy to achieve a structure where the solid column in the inner cyclone return lug extends higher than the solid column formed by the product solids separated by the outer cyclone downward return lug. The solid column must be maintained if the pressure in the cyclone's interior space is below atmospheric pressure around the bottom end of the cyclone's downward return lug. If the bottom end of the downward return lug of the cyclone opens into the same space, the difference in height at the top of each solid column is necessary to compensate for the pressure difference in the interior space of each cyclone. The pressure difference in the interior space of each cyclone is mainly caused by the pressure drop caused by the guide vanes or similar deflecting means, and the pressure loss and flow velocity changes caused by the flow lugs. This pressure difference accumulates in the downward return lug of the cyclone and is compensated by a hydrostatic pressure difference on solid columns of different heights. This allows the solids to be returned to the cyclone bed using the above example. Hereinafter, embodiments of the present invention will be described with reference to the accompanying drawings.

[0026]

EXAMPLE 1 FIGS. 1 (b) and 2 (b) show first and second preferred embodiments of the present invention used in a fluidized bed catalytic cracking (FCC) facility. The FCC unit includes two reactors, one of which is a circulating fluidized bed reactor and the other is a bubbling fluidized bed regenerator. FIGS. 1A and 2A show a conventional structure used for the same purpose. FCC Reactor FIG. 1 (b) shows the cyclone structure of the present invention, and FIG. 1 (a) shows a conventional cyclone arrangement, in which two cyclones (
(Primary and secondary cyclones) are directly connected in series. Naturally, the number of cyclones connected in series may be two or more or less.

A mixture of the functional pre-fluidizing gas of the conventional cyclone arrangement and the evaporating phase of the reacted and reacting hydrocarbons is sent upwardly along the riser 12 in gaseous phase. The accompanying catalyst is conveyed to the first cyclone 13 provided in the internal space of the reaction vessel 15, and the solid catalyst is separated from the gas phase on the wall of the reaction chamber, and the solid catalyst is removed from the first cyclone 13 during the downward return lug. fall into. The dropped catalyst is sent from this return lug to the hydrocarbon separation section and the regenerator. The gas stream entering the first cyclone 13 exits the cyclone 13 through the central pipe,
Enter the second cyclone 14. The particulate matter collides with the chamber walls of this cyclone, is separated from the gas and falls into the return lug of the second cyclone 14. The gas discharged from the second cyclone 14 is discharged from the reaction vessel 15 through the recovery chamber through the recovery nozzle.

The cyclone assembly of the present invention and its function The reactor 11 of FIG. 1 (b) comprises a first cyclone, a second cyclone, a riser 1 for passing a reaction mixture stream to the first cyclone, and a gas. And a discharge pipe 10 for discharging the stream from the second cyclone and discharging from the entire reactor assembly 11. The first cyclone has an annular space 2 formed at the upper end of the riser 1 in the internal space of the reactor 11, a guide blade 3 provided at least above the annular space 2, and a position below the guide blade. And a downward return lug 5 connected to the lower part of the chamber 4, the reaction mixture flow passing through the guide vanes 3 is forced into a vortex-rotating flow, and flows along the inner wall of the chamber 4. Washed away.

The second cyclone is provided in an internal space of the first cyclone, and has a central pipe 6 forming an axial annular flow path for sending a gas flow introduced into the first cyclone from the first cyclone to the second cyclone. And a guide vane 7 connected to an axial annular flow path consisting of the central pipe 6 and a chamber 8 connected to the guide vane 7, all of which components enter the second cyclone. Causing a swirling motion in the flow,
Thereby, the inner wall of the chamber 8 is washed away. The second cyclone further includes a return lug 9. This return lug 9 extends downward from the chamber 8 and is preferably arranged coaxially with the interior space of the return lug 5 of the first cyclone.

In operation of the above assembly, a mixture of the pre-fluidized gas and the vaporized phase of the reacted and reacting hydrocarbons is sent upwardly along the riser 1 in the gas phase. The accompanying catalyst is carried together with the gas to the annular space 2 provided in the internal space of the reactor 11 and rises upward therefrom toward the guide blades 3 of the first cyclone. The guide vanes 3 serve to cause a vortex flow, and the entrained particles collide with the inner wall of the chamber 4 by centrifugal force and are separated from the gas flow and fall into the downward return lug 5 of the first cyclone. The separated catalyst is sent from the return lug 5 to the hydrocarbon separation section and the regenerator. The gas stream entering from the first cyclone leaves this cyclone via a central pipe 6. The gas flow further rises along the annular passage to the guide vanes 7 of the second cyclone. The particles collide with the inner wall of the cyclone chamber 8 and are separated from the gas phase and fall into the downward return lug 9 of the second cyclone. The return lug 9 of the second cyclone is the first
Is preferably provided in the internal space of the return lug 5. The gas stream sent to the second cyclone leaves the cyclone and the reactor 11 from the outlet nozzle 10.

[0031] The FCC regenerator shown in FIG. 2 (a) shows a conventional cyclone construction, in Figure 2 (b) shows a cyclone assembly according to the present invention. Both of these arrangements have two cyclones (first cyclone and second cyclone) connected in series to the interior space of the FCC regenerator.
The number of cyclones connected in series can be changed, and may be two or more, one, or may have a plurality of cyclones connected in parallel. Since the maximum diameter of a conventional cyclone is about 1 m, a plurality of conventional cyclones must generally be connected in parallel.

Conventional cyclone arrangement In this case, the air passing through the bottom grid 27 is regenerated under bubbling floor conditions by a regenerator 28.
The catalyst contained therein is fluidized to supply oxygen required for the coke combustion reaction. This gas stream containing suspended particles passes through a first cyclone 29 provided in the interior space of the regenerator 28. The particles in this stream impinge on the inner walls of the separation chamber and are separated from the gas phase and fall into the downward return lug 29 of the first cyclone 29. That is, the separated catalyst is returned to the fluidized bed from the return lug. The gas flow entering from the first cyclone 29 leaves the cyclone 29 via the central pipe and passes through the second cyclone 3
Sent to 0. The particles collide with the inner wall of the cyclone and are separated from the gas phase and fall on the downward return lug of the second cyclone 30. The gas stream passes from the second cyclone 30 through the collection chamber and finally leaves the reactor from outlet nozzle 31.

The cyclone assembly of the present invention and its function The regenerator 18 of FIG. 2B comprises a first cyclone, a second cyclone, a grid 17 for sending air to the regenerator, a second cyclone and And a discharge nozzle 26 for discharging a gas flow from the entire regenerator 18. The first cyclone includes a guide vane 19 provided at least above a cyclone chamber in the internal space of the regenerator 18, and a chamber 20 located below the guide vane 19. The guide vanes 19 serve to forcibly rotate the gas flow entering the chamber to wash the inner wall of the chamber. The first cyclone further has a downward return lug 21 connected to the lower part of the chamber 20.

The second cyclone is provided in an internal space of the first cyclone, and has a central pipe 22 that forms an axial annular flow path that passes a gas flow introduced into the first cyclone from the first cyclone to the second cyclone. , Having a guide vane 23 connected to an axial annular flow path formed by the central pipe 22 and a chamber 24 connected to the guide vane 23, all of which components enter the second cyclone. The gas flow is swirled to wash the inner wall of the chamber 24. The second cyclone further has a return lug 25 extending downward from the chamber 24. This lug 25 is preferably arranged coaxially with the inner wall of the return lug 21 of the first cyclone.

When operating this assembly, the inlet air through the grid 17 at the bottom is
The catalyst contained in 8 is fluidized to a bubbling bed state, and at the same time, oxygen necessary for the coke combustion reaction is supplied. The gas flow containing the suspended catalyst particles rises and enters the guide vanes 19 formed in the internal space of the first cyclone. The function of the guide vanes 19 is to create a vortex flow and cause the particles to impinge on the inner wall of the chamber 20 by centrifugal force to separate from the gas phase and drop on the downward return lug 21 of the first cyclone. The dropped catalyst is returned from the return lug 21 to the fluidized bed. The gas flow entering the first cyclone 29 leaves the cyclone via the central pipe 22. The gas flow further rises along the channel of annular cross section and enters the guide vanes 23 of the second cyclone. The particles collide with the inner wall of the chamber 24 of the cyclone and are separated from the gas phase and fall on the downward return lug 25 of the second cyclone. The return lug 25 of the second cyclone is the first
It is advantageously provided in the interior space of the return lug 21 of the cyclone. The gas stream leaves the cyclone and regenerator from second cyclone 30 via outlet nozzle 26.

Embodiment 2 This embodiment will be described using a conventional single-port cyclone and the multi-port cyclone of the present invention. FIG. 3A shows a conventional connection method between the first cyclone and the second cyclone. FIG. 3 (b) shows the connection method of the present invention, wherein the multi-port cyclone is completely contained in the internal space of the single-port cyclone. The installation of the multi-port cyclone inside the single-port cyclone makes it possible to symmetrically distribute the gas flow in the interior space of the cyclone, so that the gas flow is symmetrically divided into the guide vanes of the second cyclone. It becomes possible.

The assembly shown in FIG. 3B comprises a single-port first cyclone chamber 46,
It has a nozzle 40 for feeding the reaction mixture stream to the cyclone chamber 46, a return lug 44 extending downward from the cyclone chamber 46, and a second multi-port cyclone provided in the internal space of the cyclone chamber 46. I have. The second cyclone includes a center pipe 41, a guide vane 42 connected to the center pipe, a cyclone chamber 43 downstream of the gas flow following the guide vane 42, and a return lug 47 extending downward from the cyclone chamber 43. And a discharge nozzle 45 extending upward from the cyclone chamber 43. The assembly shown in FIG. 4 is substantially similar to the assembly of FIG. 3 (b), except that a second cyclone is provided in a portion above the first cyclone. For this reason, a high hydrostatic pressure difference can be created between the solid column included in the return lug 44 and the solid column included in the return lug 47. The second cyclone guide vanes 42 are provided only in a part of the inside of the center pipe 41.

[Brief description of the drawings]

FIG. 1 is a diagram showing a cyclone (b) according to a first embodiment of the present invention and a conventional cyclone (a) used for the same application.

FIG. 2 is a diagram showing a cyclone (b) according to a second embodiment of the present invention and a conventional cyclone (a) used for the same application.

FIG. 3 is a diagram showing a cyclone (b) according to a third embodiment of the present invention and a conventional cyclone (a) used for the same application.

FIG. 4 shows an embodiment of the cyclone of the present invention assembled such that a greater hydrostatic pressure difference occurs in the embodiment of FIG. 3 between the inner and outer cyclones. In this embodiment, the guide vanes are provided only in part of the interior of the inlet chamber and can utilize the tangential velocity component imparted to the flow by the primary cyclone.

[Procedural Amendment] Submission of translation of Article 34 Amendment of the Patent Cooperation Treaty

[Submission date] November 10, 2000 (2001.10.10)

[Procedure amendment 1]

[Document name to be amended] Statement

[Correction target item name] Claims

[Correction method] Change

[Correction contents]

[Claims]

2. The method according to claim 1 , wherein the material stream to be treated comprises gases, liquids and / or solids.

3. The process as claimed in claim 1 or 2 material flow to be treated contains a solid in suspension.

Claims410. The material stream to be treated is a liquid stream containing solids to be removed. 2 The method described in.

5. The process according to claim 3, wherein the gas stream to be treated comprises flue gas emitted from the coke combustion process, the flue gas comprising the catalyst to be regenerated in suspended particulate form.

6. A treated by the gas flow the gas to be treated, the method of claim 3 wherein the gas products of the fluidized catalytic process containing a liquid component and / or solids.

7. The method of claim 6 fluidized catalytic process is a catalytic cracking process of hydrocarbons carried out in a fluidized bed catalytic cracking facilities.

8. A gas stream to be treated is flue gas from the boiler of the energy generating device, The method of claim 3, the flue gas contains particulate matter to be removed.

9. gas flow to be treated is an exhaust gas of the drying process, The method of claim 3, the exhaust gas contains particulate matter to be removed.

[Claim 1 0] gas stream to be treated is an exhaust gas of a steam system, The method of claim 3, the exhaust gas contains particulate matter to be removed.

[Claim 1 1] The method according to any one of claims 1 to 10 using a plurality of cyclones connected in series to the material of the first phase to separate the material of the second phase.

[Claim 1 2] connects two to five cyclones in series, according to claim 1 1, preceding the downward return downstream of any one cyclone in the cyclone provided in the lug has a downward return lug the method of.

[Claim 1 3] The method according to at least two of any one of successive cyclones claims adapted to discharge the solids into a common space 1 and 1 2 are connected in series.

Is connected to the claim 1 4] series, claim 1 to maintain by changing the height of the solids column in the downward return lag compensating the cyclone pressure difference between the interior space of the successive cyclone for discharging the solid to the same space 3. The method according to 3 .

[Claim 1 5] material flow is fed to the multi-port cyclone through the supply nozzle, the stream entering from the outside of the cyclone in the interior space of the multiport cyclone, guided by a deflecting means provided on the supply nozzles are deflected, all or at least some a method according to any one of claims 1 to 1 4 positioned outside the cyclone of this deflection means.

With claim 1 6] deflecting and / or guiding means such as a tubular guide member including a second cyclone guide vane members for guiding and deflecting the flowing stream upwardly provided on the outer surface, the flow is first 2. The material stream is directed to a second multi-port cyclone so as to flow upward from the first cyclone to a top edge of the second cyclone.
The method according to any one of claims 1 to 15 .

[Claim 1 7] material flow feeding the first multiport cyclone to a second multiport cyclone flow with deflection and / or guide means provided on the outer surface of the second cyclone guide of the first cyclone The method of claim 16 wherein the flow is from below the vane member to a second cyclone guide vane member located above the first cyclone guide vane member.

18. following a) ~d): a) separation chambers, each almost vertically aligned (4,8; 20, 24; 43, 46
B) at least one first and second separating means, wherein the second separating means is inside the first separating means; b) a material stream to be treated, connected to the separating means. Supply nozzle (1; 17; 4)
0), c) an outlet nozzle (10; 26; 45) connected to at least one separating means for discharging a stream of material to be treated from said separating means, d) provided at least inside the first separating means. The material stream provided in the separating means provided is forcibly rotated in a vortex, and the inner wall of the separating chamber (4,8; 20,24; 43) is washed away and the gas, liquid and / or A guide vane (3,7; 19,23; 42) for separating solids from a material stream, the assembly for separating gases, liquids and / or solids from a material stream of a fluidized catalytic processor . The method wherein the separating means is a multi-port cyclone .

19. The separation chamber when viewed at right angles to the vertical center axis of the inner chamber wall according to claim (4,8; 20, 24 43, 46) has a substantially circular cross-section 18
An assembly according to claim 1.

20. Guide vanes (3,7; 19,23; 42) comprising radially directed baffles which are arranged around a vertical central axis of a separation chamber (4,8; 20,24; 43). And a separation chamber (4, 8; 2) for the material stream to be treated.
20. Assembly according to claim 18 or 19 , wherein the flow path to (0,24; 43) is divided into parallel partial flows.

21. A parallel partial flow is created by a radial baffle plate provided between two coaxially mounted cylindrical shells, the baffle plate being aligned parallel to the longitudinal axis of the reactor space. the assembly of claim 2 0.

2. 2] least supply nozzles one of the separating means has a generally annular cross-section provided in the interior space of the first separating means (2,6; 22; 41) provided with this supply nozzle material flow 22. The assembly according to any one of claims 18 to 21 , which supplies to the guide vanes (3, 7; 23; 42) and from there to the separation chamber (2, 6; 22; 41).

2. 3 The supply nozzle having a substantially annular cross-section (2,6; 22; 41)
Claim 2 2 but formed by mutually circular parallel supply passages are equally spaced
An assembly according to claim 1.

It includes (42 3,7; 19, 23), 2. 4] separating means guide vanes
The guide vanes force the material stream into a vortex-rotating motion, and separate the separation chambers (4,8; 2).
24) The assembly according to any one of claims 18 to 23 , wherein the inner wall of (0,24; 43) is flushed and the gas, liquid and / or solids are separated from the material stream by the action of centrifugal force.

2. 5 An assembly according to at least another any one similar second separating means is being claim 18 21 to 24 which is attached to the inside of the second separation means.

And 26. The first separating means, each of the second separating means mounted in the inner space of the first separation means, serves to return the separated solids from the separating means into a common collection space 18. with a downward return lugs provided coaxially to ~
An assembly according to any one of claims 25 .

27. back lugs of any internal separation means in the vertical direction, the assembly of claim 26 which extends to above the upper edge of the nearest preceding coaxial outer separating means.

28. At least a portion of the guide vanes of the separating means is provided outside and above the separation means, from the outside of the separation means according to claim 23-27, which extend radially inward until it reaches the inner space of the separating means An assembly according to any one of the preceding claims.

29. At least the guide vanes of the separation means attached downward so as to wrap the outer surface of and separating means mounted in the inner space of the first separation means (3,
7; 19, 23; 42) comprising a deflecting and / or guiding means, such as a tubular guiding member, which deflects and / or guides the material stream to be processed in an upright direction from the bottom of the outer separating means. claim flow into the guide vanes of the inner separating means subsequent 18
An assembly according to any one of to 2 8.

3. 0] deflecting and / or guiding means assembly according to claim 29 having a guide vane member provided in the guide means for guiding and deflecting the stream flowing upward.

31. At least two coaxially mounted multiports as separating means, characterized in that the guide vanes of each inner cyclone which are continuous with one another are provided above the guide vanes of the preceding outer multiport cyclone. 31. The assembly according to any one of claims 18 to 30 , comprising a cyclone.

──────────────────────────────────────────────────続 き Continued on the front page (51) Int.Cl. ⁷ Identification symbol FI Theme coat ゛ (Reference) B04C 5/24 B04C 5/24 B07B 7/08 B07B 7/08 C10G 11/18 C10G 11/18 (81) Designated countries EP (AT, BE, CH, CY, DE, DK, ES, FI, FR, GB, GR, IE, IT, LU, MC, NL, PT, SE), OA (BF, BJ, CF, CG, CI, CM, GA, GN, GW, ML, MR, NE, SN, TD, TG), AP (GH, GM, KE, LS, MW, SD, SL, SZ, UG, ZW), E A (AM, AZ, BY, KG, KZ, MD, RU, TJ, TM), AE, AL, AM, AT, AU, AZ, BA, BB, BG, BR, BY, CA, C , CN, CR, CU, CZ, DE, DK, DM, EE, ES, FI, GB, GD, GE, GH, GM, HR, HU, ID, IL, IN, IS, JP, KE, KG, KP, KR, KZ, LC, LK, LR, LS, LT, LU, LV, MD, MG, MK, MN, MW, MX, NO, NZ, PL, PT, RO, RU, SD, SE, SG , SI, SK, SL, TJ, TM, TR, TT, UA, UG, US, UZ, VN, YU, ZA, ZW (72) Inventor Niemi, Vesa Finland 06400 Porvov Velajapolk 1D F-term ( Reference) 4D021 FA25 4D031 AC04 BA01 DA01 4D053 AA03 AB01 BA05 BB01 BC01 BD04 CA04 CA15 4D071 AA53 4H029 BD08 BD19

Claims (35)

[Claims] 1. A process material stream comprising a first phase material and a suspended or dispersed second phase material is passed through at least one first separation means and then to at least one second separation means. A method for separating two phases from each other by separating the suspended or dispersed phase material from the first phase material by centrifugal force, wherein at least one unit of the second separation means is a multi-port cyclone. A method wherein the multi-port cyclone is provided inside the first separating means and feeds the material stream to be treated into the cyclone via a feed nozzle having an annular cross section. 2. The method according to claim 1, wherein a multi-port cyclone is used as the first separating means. 3. A single port cyclone as the first separating means.
The method described in. 4. The method according to claim 1, wherein the material stream to be treated comprises a gas, a liquid and / or a solid. 5. The process according to claim 1, wherein the material stream to be treated comprises solids in suspension. 6. The method according to claim 4, wherein the material stream to be treated is a liquid stream containing solids to be removed. 7. The method according to claim 5, wherein the gas stream to be treated comprises flue gas emitted from the coke combustion process, wherein the flue gas comprises the catalyst to be regenerated in suspended particulate form. 8. The process according to claim 5, wherein the gas stream to be treated is a gas product of a fluidized catalytic process comprising a gas to be treated, a liquid component and / or a solid. 9. The method of claim 8, wherein the fluidized catalyst process is a hydrocarbon catalytic cracking process performed in a fluidized bed catalytic cracking facility. 10. The method of claim 5, wherein the gas stream to be treated is flue gas from a boiler of an energy generator, wherein the flue gas contains particulate matter to be removed. 11. The method according to claim 5, wherein the gas stream to be treated is the exhaust gas of a drying process, the exhaust gas comprising the particulate matter to be removed. 12. The method according to claim 5, wherein the gas stream to be treated is the exhaust gas of a steam system, the exhaust gas containing the particulate matter to be removed. 13. The method according to claim 1, wherein a plurality of cyclones connected in series are used to separate the second phase material from the first phase material. 14. The method according to claim 13, wherein two to five cyclones are connected in series, and any one of the downstream cyclones provided inside the preceding downward return lug has a downward return lug. . 15. The method according to claim 1, wherein at least two consecutive cyclones connected in series discharge solids into a common space. 16. The method according to claim 15, wherein the compensation of the pressure difference in each internal space of successive cyclones connected in series and discharging solids into the same space is maintained by changing the height of the solid column of the cyclone downward return lugs. The described method. 17. A flow of material is sent to a multi-port cyclone via a supply nozzle, and a flow entering the internal space of the multi-port cyclone from outside the cyclone is guided and deflected by a deflecting means provided in the supply nozzle. 17. The method according to any of the preceding claims, wherein all or at least a part of the deflection means is located outside the cyclone. 18. The method according to claim 18, wherein the flow is performed by using a deflecting and / or guiding means such as a tubular guide member including a guide vane member provided on an outer surface of the second cyclone for guiding and deflecting the upward flowing flow. The material stream is directed to a second multi-port cyclone so as to flow upward from the cyclone to a top edge of the second cyclone.
18. The method according to any one of claims 17 to 17. 19. A stream of material is sent from a first multi-port cyclone to a second multi-port cyclone, wherein the flow is guided by means of deflection and / or guide means provided on the outer surface of the second cyclone. 19. The method of claim 18, wherein the flow is from below the member to a guide blade member of a second cyclone located above a guide blade member of the first cyclone. 20) The following a) to c): a) Separation chambers (4, 8; 20, 24; 43, 46), each of which is substantially vertically aligned.
B) at least one first and second separating means having a), b) a feed nozzle (1; 17; 4) of the material stream to be treated, which is connected to the separating means
0), c) flowing a gas, liquid and / or solid having an outlet nozzle (10; 26; 45) connected to at least one separation means for discharging a stream of material to be treated from said separation means. An assembly for separating from a material stream of a catalytic treatment unit, characterized by the following i), ii): i) at least one second separating means is provided inside the first separating means; ii) at least a separating means provided inside the first separating means forcibly vortexing the material stream, flushing the inner walls of the separating chamber (4,8; 20,24; 43), It has guide vanes (3,7; 19,23; 42) which in operation separate gas, liquid and / or solid from the material stream. 21. The separation chamber (4,8; 20,24; 43,46) has a substantially circular cross section when viewed perpendicular to the vertical center axis of the chamber inner wall.
An assembly according to claim 1. 22. Guide vanes (3,7; 19,23; 42) comprising radially directed baffles which are arranged around a vertical central axis of the separation chamber (4,8; 20,24; 43). And a separation chamber (4, 8; 2) for the material stream to be treated.
22. Assembly according to claim 20 or 21, wherein the flow path to (0, 24; 43) is divided into parallel partial flows. 23. A parallel partial flow is created by a radial baffle plate provided between two coaxially mounted cylindrical shells, the baffle plate being aligned parallel to the longitudinal axis of the reactor space. An assembly according to claim 22. 24. At least one separating means provided in the interior space of the first separating means comprises a feed nozzle (2, 6; 22; 41) having a substantially annular cross section, said feed nozzle directing a material stream. 24. The assembly according to any one of claims 20 to 23, which feeds the guide vanes (3,7; 23; 42) and from there to the separation chamber (2,6; 22; 41). 25. A supply nozzle (2, 6; 22; 41) having a substantially annular cross section.
25 are formed by equally-spaced parallel supply passages which are circular to each other.
An assembly according to claim 1. 26. The separating means includes guide vanes (3, 7; 19, 23; 42);
The guide vanes force the material stream into a vortex-rotating motion, and separate the separation chambers (4,8; 2).
An assembly according to any one of claims 20 to 25, wherein the inner wall of (0,24; 43) is flushed and gas, liquid and / or solids are separated from the material stream by the action of centrifugal force. 27. The assembly according to claim 20, wherein a multi-port cyclone is used as the first separating means. 28. The assembly according to claim 20, wherein a single port cyclone is used as the first separating means. 29. An assembly according to any of claims 20 to 28, wherein at least another similar second separating means is mounted inside the second separating means. 30. Each of the first separation means and each of the second separation means attached to the internal space of the first separation means plays a role of returning separated solids from the separation means to a common recovery space. 21. A downward return lug provided coaxially with
30. The assembly according to any one of claims 29. 31. The assembly according to claim 30, wherein the return lug of any vertical internal separating means extends above the top edge of the nearest preceding coaxial outer separating means. 32. The separating means according to claim 20, wherein at least a part of the guide vanes of the separating means is provided outside and above the separating means, and extends radially inward from outside the separating means to reach the internal space of the separating means. An assembly according to any one of the preceding claims. 33. At least the guide vanes (3, 3) of the separating means mounted in the interior space of the first separating means and mounted downward so as to enclose the outer surface of the separating means.
7; 19, 23; 42) comprising a deflecting and / or guiding means, such as a tubular guiding member, which deflects and / or guides the material stream to be processed in an upright direction from the bottom of the outer separating means. 21. Flow to the guide vanes of the subsequent inner separating means.
An assembly according to any one of claims to 32. 34. The assembly according to claim 33, wherein the deflecting and / or guiding means comprises guide vanes provided on the guiding means for guiding and deflecting the upwardly flowing flow. 35. At least two coaxially mounted multiport cyclones as separating means, characterized in that the guide vanes of each inner cyclone which are continuous with one another are provided above the guide vanes of the preceding outer multiport cyclone. An assembly according to any one of claims 20 to 34, comprising: